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TDA Research Inc. • Wheat Ridge, CO 80033 • www.tda.com
Integrated WGS Reactor/CO2 Capture System for Pre-combustion Carbon Capture
(Contract No. DE-FE-0023684)
Gökhan Alptekin Ambal Jayaraman
Mike Bonnema
DOE/NETL Project Kick-off Meeting
January 9, 2014
TDA R e s e a r c h 2 2
• Privately Owned / Began operations in 1987 • 82 full-time technical staff
• Primarily chemists and engineers, more than half with advanced degrees (28 PhDs)
TDA Research, Inc.
Wheat Ridge Facility
Golden Facility
12345-12355 W 52nd Avenue
22,000 ft2 offices and labs Synthetic Chemistry, Catalyst/Sorbent Synthesis and Testing, Machine and Electronics Shops, SEM, TOF Mass Spec
4663 Table Mountain Drive 27,000 ft2 offices and labs 27 fume hoods, Synthetic Chemistry,
Catalytic Process Development
2
TDA R e s e a r c h 3
TDA Products - Licences
Direct Oxidation for Bulk Sulfur Removal
Licenses with SulfaTreat DO and GTC (1.3 and 6 ton/day plants at Bakersfield, CA)
Fullerene Synthesis License with Frontier Carbon
40 ton/year plant in Kitakyushu, Japan TDA built the reactors
• Technologies with high capital investment requirement commercialized via licensing/strategic partnerships
TDA R e s e a r c h 4
TDA Products – Direct Sales
OligotronTM - Conducting polymers available through
Sigma-Aldrich Ambient Temperature CO Oxidation Catalyst
SuperSoapTM
TDA R e s e a r c h
Reactor Development
5 5
TDA Spin-off - SulfaTrapTM Sorbents
SulfaTrapTM sorbents for stationary/mobile fuel cell applications • SulfaTrapTM sorbents
desulfurizes various gas streams • Natural gas, LPG, biogas,
reformate gas desulfurization, diesel fuel, logistics fuel
• ~50% of fuel cells installed globally (MCFC, SOFC and PEM fuel cells) uses SulfaTrapTM products
5
TDA R e s e a r c h
Project Objective • The objective is to demonstrate techno-economic viability of an
integrated WGS catalyst/CO2 removal system with thermal management used in an IGCC power plant • A high temperature PSA adsorbent for CO2 removal above the dew
point of the synthesis gas • A commercial low temperature water-gas-shift catalyst • Heat removal/recovery using a membrane evaporator (or a direct water
injector) • Project Tasks
• Design and fabrication of an integrated WGS/CO2 removal system (15 kg/hr CO2 removal capability)
• Bench-top evaluation of material performance for 30,000 cycles • Evaluate the best design in a slipstream test at NCCC using coal
derived syngas • Evaluate the best design in a slipstream test at the Wabash River IGCC
plant using coal derived syngas • A high fidelity engineering design and cost analysis
6
TDA R e s e a r c h
Project Partners
7
Project Duration • Start Date = October 1, 2014 • End Date = September 30, 2017 Budget • Project Cost = $5,632,619 • DOE Share = $4,506,719 • TDA and its partners = $1,125,900
TDA R e s e a r c h
TDA’s Approach
8
• A high temperature CO2 adsorbent is combined with a low temperature shift catalyst for complete shifting of CO at low steam:carbon ratios
• Traditional approach used multi-stage WGS reactors with inter-stage cooling • WGS is an equilibrium-limited exothermic reaction
• Water is supplied at concentrations well above required by the reaction stoichiometry to completely shift the CO to CO2
3-stage WGS unit as described in the DOE/NETL-2007/1281
TDA R e s e a r c h
Expected Benefits
9
• Reducing the need to raise excess quantities of steam improves the power cycle efficiency
• Water in the synthesis gas is useful but to a point • It reduces the gas turbine temperature and prevents NOx
formation • The removal of CO2 reaction product will shift the WGS reaction
equilibrium even at low steam:carbon ratios CO + H2O = H2 + CO2
• Lower energy consumption to raise steam • Process intensification reduces the number of hardware
components and cost
Sorbent’s point of view: • Less dilution w/water higher CO2 partial pressure
TDA R e s e a r c h
TDA’s Approach to Sorbent
10
• The sorbent consists of a mesoporous carbon modified with surface functional groups that remove CO2 via strong physical adsorption • CO2-surface interaction is strong enough to allow operation at
elevated temperatures • Because CO2 is not bonded via a covalent bond, the energy input for
regeneration is low • Heat of CO2 adsorption is measured as 4.9 kcal/mol for TDA
sorbent • Selexol ~4 kcal/mol • Amine solvents ~14.4 kcal/mol • Chemical absorbents 20-40 kcal/mol (Na2CO3NaHCO3 30 kcal/mol)
• Net energy loss in sorbent regeneration is similar to Selexol • A much better IGCC efficiency due to high temperature CO2 capture • Warm gas clean-up improves cycle efficiency 2 to 4%
TDA R e s e a r c h
Integrated WGS/CO2 Capture System
11
TDA R e s e a r c h
Operating Conditions
12
• Isothermal operation is critical to eliminate heat/cool transitions which reduces cycle time and increases sorbent utilization
• Steam consumption can be significantly reduced if steam purge is carried out at low pressure
• Commercial WGS catalyst (Shiftmax 230) is co-located with the sorbent
TDA R e s e a r c h
Application to CTL
CTL
Liquids
CTL
TDA R e s e a r c h
Technology Status/R&D Needs
14
• Sorbent is developed under a separate DOE project (DE-FE0000469)
• WGS catalyst is commercially available • Early-stage concept demonstration has already been completed
(under DE-FE0007966) • Integrated sorbent/catalyst operation
• Early-stage prototype demonstration of an integrated system with heat management is also under progress (under DE-FE-00012048) • ~0.2 kg/hr CO2 removal • Slipstream test at the NCCC
• Key R&D need is the design/development of a high fidelity prototype to fully demonstrate the concept using actual coal-derived synthesis gas
TDA R e s e a r c h
Previous Work Sorbent Development
DE-FE0000469
15
TDA R e s e a r c h
TDA’s Sorbent A mesoporous carbon is
used to disperse the active sorbent phase
Pore size can be finely tuned in the 10 to 100 A range
Mesopores eliminates diffusion limitations and rapid mass transfer, while enables high surface area
The preparation process also enables us to introduce various surface groups active for removing different compounds
0
0.5
1
1.5
2
0 10 20 30 40 50 60 70 80 90 100 110 120
Diff
eren
tial P
ore
Volu
me
(cm
3 /g)
Pore Width (Angstroms)
AMS 62A AMS 62B AMS 62C
16
US Pat. Appl. 61787761, Dietz, Alptekin, Jayaraman “High Capacity Carbon Dioxide Sorbent” US Pat. Appl. 61790193, Alptekin, Jayaraman, Copeland “Pre-combustion Carbon Dioxide Capture System Using a Regenerable Sorbent”
TDA R e s e a r c h
Lower pressureregenerations
Analyzer Drift
Multiple Cycle Tests – Bench-scale
H2=32%, CO2=40%, N2=3%, CO=1%,H2O=24%; T= 240oC; Pads= 500 psig; Pdes = 50-300 psig
• Sorbent maintained its CO2 capacity (8+%wt.) for 12,650 cycles
CO2 Capacity
17
CO2 Removal Efficiency
TDA R e s e a r c h
Slipstream Demonstrations
Wabash River IGCC Plant, Terre Haute, IN • Demonstration carried out in September 2012 • Largest single-train Gasifier (262 MW) • Oxy-blown E-GasTM Gasifier • Operates on petcoke
18
National Carbon Capture Center, Wilsonville, AL • 1st Demonstration carried out in November, 2011 • 2nd Demonstration carried out in April, 2012 • Pilot-scale air blown TRIG gasifier • Operates on low rank coals
• Several for proof-of-concept tests were completed at two different facilities
TDA R e s e a r c h
Test Units – In NEMA-Rated Enclosures CO2 Removal Skid
Gas Conditioning Skid
19
TDA R e s e a r c h
Field Test Units Installed at NCCC
20
TDA R e s e a r c h
Field Test Units at Wabash River IGCC
21 TDA Proprietary
TDA R e s e a r c h
Prototype Performance
• Sorbent achieved similar CO2 capacity before and after the field test • 2.6% wt. CO2 at PCO2 = 38 psi
• Prototype unit under Wabash condition (PCO2 = 140 psi) achieved 4.1% wt. CO2 capacity
• Next generation E-Gas gasifier is expected to operate at 750 psi (PCO2 = 240 psi) and capacity will exceed 10% wt. CO2 22
TDA R e s e a r c h
System Analysis Results
• IGCC plant with TDA’s CO2 capture system achieves higher efficiency (34.0%) than IGCC with SelexolTM (31.6%)
• Cost of per tonne CO2 avoided is $31.12 for TDA’s warm gas CO2 capture technology compared $49.50 for cold gas cleanup with SelexolTM technology
23
TDA R e s e a r c h
0.1 MW Slipstream Demonstration
24
Water Gas ShiftCatalyst Bed
Sulfur Beds
Control Panel
Recycle compressor
CO2 Separation Skid
Gas Processing Skid
• 0.1 MW demonstration at Sinopec’s Fujian ethylene complex • Asphaltene fractions/petcoke feed
TDA R e s e a r c h
Gas Conditioning Skid
25
LTWGS Bed
HTWGS Bed
Desulfurization Beds
N2 Pre-heater
Sulfur Polishing Bed
Integrated Service Scaffold
LabVIEW Control 24” Inspection Manway
TDA R e s e a r c h
CO2 Separation Skid
26
CO2 Sorbent Beds (8)
Gas Analyzers
20-Zone Heater Control
LabVIEW Control System
Accumulators
Re-circulating Chiller
N2 Pre-heater Flow/Pressure
Control Valves
TDA R e s e a r c h
25’
11’6”
7’6”
CO2 Separation Skid
27
14” OD x 8ft 200 L 304 SS Rated 450°C/ 750 psig
TDA R e s e a r c h
Previous Work Integrated WGS/CO2 Capture
Concept Demonstration DE-FE0007966
28
TDA R e s e a r c h
Bench-scale Evaluations
29
• We carried out multiple cycle tests with combined WGS catalyst and CO2 sorbent using partially shifted synthesis gas • CO concentration climbed up to equilibrium level only after sorbent
reached its CO2 capacity • The sorbent and the catalyst maintained their performance over 1240
cycles breakthrough data
TDA R e s e a r c h
NCCC – 2nd Field Test
30
• Prototype system achieved 90+% carbon capture under Steam:CO ratio of 1:1.1 with average CO conversion of 96.4%
TDA R e s e a r c h
Reaction Exotherm During Field Test
31
• Reaction exotherm was evident even in small reactors (which are prone to more heat losses)
TDA R e s e a r c h
Reactor Design Concepts
32
Concept #1 Concept #2
TDA R e s e a r c h
Reactor Design
33
Substrate Pore
PressurizedWater
SubstrateCO2 Sorbent +WGS Catalyst
ΔHads+ ΔHrxncreates steam at substrate
surface
Conventional Internally-cooled Fixed-Bed Reactors
Current Concept In addition to take advantage of the
conductive cooling takes advantage of evaporative/convective cooling
TDA R e s e a r c h
Heat Wave During CO2 Capture Only
34
Gas flow
• Adsorption heat wave results which gets canceled during desorption
t = 0 s t = 30 s t = 60 s t = 90 s t = 120 s
TDA R e s e a r c h
Heat Wave WGS & CO2 Capture
35
Gas flow
• Combined WGS & CO2 capture results in higher ∆T and the beds are not ideal for CO2 capture (the WGS heat accumulates in the beds)
TDA R e s e a r c h
Heat Integrated WGS & CO2 Capture
36
Gas flow
• When using steam introduction at three different locations in the beds the maximum temperature in the beds can be reduced from 245 to 230°C
TDA Proprietary
TDA R e s e a r c h
Early-stage Evaluations
37
• 8L reactor was modified with the permeable tube design
• Testing under once through flow
• Water flows through all or some of the 6 tubes positioned perpendicular to the syngas flow
• Successful proof-of-concept demonstrations • Several problems
• Control of water injection rate (which reduces the temperature early in the adsorption process)
• Steam loss to the regeneration side
TDA R e s e a r c h
Scope of Work
38
Budget Period 1 (BP1: 10/1/2014 – 9/30/2015) Design a field test unit including detailed design of the sorbent reactors,
using multi-component adsorption and CFD simulation models Have the input and full approval of NCCC and CB&I Complete sorbent manufacturing based on the current Manufacturing Plan Initiate a long-term sorbent life evaluation (8,000 cycles) Budget Period 2 (BP2: 10/1/2015 – 9/30/2016) Complete evaluation of single integrated reactor with simulated syngas Revise our reactor design based on results from single reactor tests Complete fabrication of the slipstream test unit Continue long-term testing of the sorbent (20,000 cycles) Budget Period 3 (BP3: 10/1/2016 – 9/30/2017) Complete long-term testing of the sorbent (30,000 cycles) Complete field tests at the NCCC and Wabash River IGCC Plants Complete a high-fidelity system design/analysis and cost estimate Complete an Environmental, Health and Safety (EHS) assessment
TDA R e s e a r c h
Project Work Plan and Schedule
39
TDA R e s e a r c h
Task 1. Project Management & Planning
40
Undertake necessary activities to ensure coordination and planning of the project with DOE/NETL and other project participants
Monitor and control the project scope, cost, schedule, and risks, Submit and get approval for the required NEPA documentation Maintain and revise the Project Management Plan (PMP) and
manage and report on activities in accordance with the plan Update the Project Management Plan as the project progresses,
and report progress against milestones, schedule and budget, including any variances
Prepare and deliver required reports and briefings
TDA R e s e a r c h
Task 2. Detailed Design of the Test Skid
41
Slipstream test unit will be designed to treat 300 SLPM of synthesis gas flow 15 kg/hr CO2 capture capability (based on the
gas flow at the Wabash River IGCC Plant) Two sub-units will be provided on separate
skids: 1) Integrated WGS/CO2 Separation Skid 2) Gas Processing Skid CO2 Separation Skid will consist of the eight
sorbent reactors, two accumulators, all valves and manifolds and a compressor that will allow recycle of some of the process gases
This will allow us to fully demonstrate the PSA cycle with all steps in the sequence (e.g., pressure equalizations, product pressurization)
TDA R e s e a r c h
Slipstream Unit Demonstration
42
• Demonstration at PSDF in the NCCC (Wilsonville, AL) • 15 kg/hr CO2 capture demonstration at Wabash River IGCC Facility
TDA R e s e a r c h
Task 3. Design Review and Hazard Analysis
43
Details of the unit will be discussed and reviewed with the site operators to ensure that it will meet all of their facility requirements
A preliminary design of the slipstream test unit will be submitted to the site operators
We will complete a Hazard Design Review with the NCCC and CB&I, to identify all safety precautions that must be included into the design
We will obtain the necessary approval from site operators to proceed with the fabrication of our slipstream test unit
TDA R e s e a r c h
Task 4. Sorbent Manufacturing
44
All the material needed for the field unit will be produced at 100 L batch size using semi-continuous/continuous manufacturing equipment in our pilot-scale production facility in Golden, CO 500 L of sorbent material to support both field demonstrations
Each batch will be characterized via physical and chemical analysis (e.g., surface area, pore size distribution, chemical composition, crush strength) to ensure that the properties meets our Product Specification Criteria
Continuous rotary kiln
Feeder
Exhaust gas treatment
TDA R e s e a r c h
Task 5. Sorbent/Catalyst Evaluation
45
The samples from each production batch will be evaluated using a bench-top reactor (1.3 L volume) with the commercial WGS catalyst
Demonstrate performance under a baseline test condition for 500 cycles
TDA R e s e a r c h
Task 6. Optimization of Reactor Design
46
Utilize CFD models for optimum integration of the WGS catalyst, CO2 separation sorbent and heat rejection system
Task 6.1 Optimization of Heat Rejection System Evaluate various reactor geometries and key process parameters
(e.g., regeneration time, product purity) using a 2D model Task 6.2 CFD Simulation
For the best design, generate detailed transient 3D concentration and temperature profiles
Using a FLUENT code, we will explore all local heat and mass transfer processes and develop axial and radial temperature and concentration profiles across the bed
Task 6.3 Optimization of Cycle Sequence Optimize the cycle sequence to ensure highest CO2 product purity
and highest H2 recovery based on the CFD results
TDA R e s e a r c h
Task 7. Long-term Durability Tests up to 8,000 Cycles
47
Bench-scale tests will be conducted to assess sorbent life Sorbent has an estimated replacement cycle of every 2 years,
which corresponds to 52,500 cycles (based on 20 minute full cycle) Due to budget and schedule constraints, the planned field test will
not be sufficiently long to fully evaluate the sorbent life Long term durability of the sorbent will be carried out under
representative temperature and pressure conditions. 5 SLPM simulated synthesis gas flow
8,000 adsorption/regeneration cycles on the sorbent in BP1
TDA R e s e a r c h
Task 8/9. Fabrication/Evaluation of a Single Test Reactor
48
We will fabricate a single reactor and evaluate the performance using simulated gas
TDA R e s e a r c h
BP1 – Milestone Log
49
BP ID Task No. Title Description
Planned Completi- on Date
Verification Method
Anticipated Project Start Date 10/12014
1 1-1 1 Update Project Management Plan (PMP)
Update PMP with inputs from DOE Project Manager 11/1/2014 PMP file
1 1-2 2 Kickoff meeting Kickoff Meeting at NETL 12/1/2014 Presentation file
1 1-3 3 Preliminary Design Package
Provide preliminary design package to field test site operators for feedback
6/30/2015 P&ID & interface requirements
1 1-4 4 Initial Design Review and Hazard Analysis
Complete initial design review and HAZOP 9/30/2015 Site approval letters
for TDA skid design
1 1-5 5 Sorbent Manufacturing Complete the production of sorbent needed for field tests 9/30/2015 Quality Assurance
Data for sorbent
1 1-6 6 Reactor design Optimizations
Complete reactor design optimizations 9/30/2015 3-D drawings of
optimized design
1 1-7 7 Long-term Durability Target I
Complete up to 8,000 cycles at bench-scale 9/30/2015 Results update
1 1-8 1 Annual Review Meeting Present the BP1 results to DOE/NETL 9/30/2015 presentation file
Go/No-go Decision Point End of Year 1 9/30/2015
TDA R e s e a r c h
BP1 – Decision Points
50
DOE funding is not authorized beyond Budget Period 1 without the written approval of the Contracting Officer
DOE’s decision whether to authorize funding for Budget Period 2 will be specifically based on: 1) Successful completion of all work proposed in the Budget Period 2) Satisfactory achievement of applicable success criteria as identified in the Project Management Plan 3) Submission and approval of the Continuation Application
Decision Point Date Success Criteria
Go/No-go Decision Point: End of Year 1 9/30/2015
Complete Final Design Package for Pilot Unit with Site Approvals.
Complete 8,000 cycles in the life test with less than 5% degradation per 10,000 cycles in sorbent performance.
TDA R e s e a r c h
BP2 - Tasks
51
Task 10. Reactor Design Revisions We will revise the CFD model and Reactor Design based on results
from single reactor evaluations Task 11. Fabrication of Revised Single Reactor We will fabricate revised reactor Task 12. Evaluation of Revised Single Reactor We will evaluate the revised reactors. Task 13. Long-term Durability Tests up to 20,000 cycles 20,000 cycles will be completed in the bench-scale unit Task 14. Critical Design Review We will complete a final design review with all site operators
TDA R e s e a r c h
BP2 – Tasks (Cont’d)
52
Task 15. Fabrication of Field Test Unit Based on the final design approved by NCCC and, CB&I, we will
fabricate the Slipstream Test Unit. Task 15.1 Fabrication of the Integrated WGS/CO2 Separation Skid:
We will construct the Integrated WGS/CO2 Separation Skid to be used in hazardous environment (i.e., Class I Division II rated)
Task 15.2 Fabrication of the Gas Processing Skid: We will construct the Gas Processing Skid, it will be designed and fabricated to allow operation in Class I Division II environment
Task 15.3 Fabrication of Process Control Module: The control system will allow stand-alone operation, with monitoring and controls to operate the system without TDA personnel being on-site
Task 16. Shakedown Testing of Gas Processing Skid We will carry out shakedown and troubleshooting of the gas
processing skid at GTI facilities
TDA R e s e a r c h
BP2 – Milestone Log
53
BP ID Task No. Title Description
Planned Completi- on Date
Verification Method
2 2-1 12 Single Reactor Evaluations
Complete Evaluation of revised singe reactor 12/31/2015 Results update
2 2-2 14 Critical Design Review Complete the final critical design review 3/31/2016
Site Approved SOP for the test
skid
2 2-3 13 Long-term Durability Target II
Complete up to 20,000 cycles at bench-scale 9/30/2016 Results update
2 2-4 15 Fabrication of Field Unit Complete the fabrication 9/30/2016 Pictures of the Skid
2 2-5 16 Shakedown Testing of Gas Processing Skid
Complete the Shakedown tests using simulated gases 9/30/2016 Results update
2 2-6 1 Annual Review Meeting Present the BP2 results to DOE/NETL 9/30/2016 presentation file
Go/No-go Decision Point End of Year 2 9/30/2016
Decision Point Date Success Criteria
Go/No-go Decision Point: End of Year 2
9/30/2016 Complete Fabrication of the Pilot Unit.
9/30/2016 Complete 20,000 cycles in the life test with less than 5% degradation per 10,000 cycles in sorbent performance.
TDA R e s e a r c h
BP2 – Decision Points
54
DOE funding is not authorized beyond Budget Period 1 without the written approval of the Contracting Officer.
DOE’s decision whether to authorize funding for Budget Period 2 will be specifically based on 1) successful completion of all work proposed in the current Budget Period, 2) satisfactory achievement of applicable success criteria as identified in the Project Management Plan, and 3) submission and approval of the Continuation Application (the Continuation Application should include a detailed budget and budget justification for budget revisions or budget items not previously justified.).
Decision Point Date Success Criteria
Go/No-go Decision Point: End of Year 2
9/30/2016 Complete Fabrication of the Pilot Unit.
9/30/2016 Complete 20,000 cycles in the life test with less than 5% degradation per 10,000 cycles in sorbent performance.
TDA R e s e a r c h
BP3 - Tasks
55
Task 17. Process Design Carry out detailed design of the integrated WGS/CO2 capture process Detailed design of the full-scale reactors and generate engineering drawings
and 3-dimensional layouts Provide an accurate cost for the unit, including all foundation work, labor and
supervision for the installed system and revise the overall system cost estimate (for a most accurate capital requirement and CO2 capture cost)
Task 18. Long-term Durability Tests up to 30,000 cycles Task 19. Shakedown Testing of the Slipstream Unit Integrate the WGS/CO2 Separation Skid and the Gas Processing Skid with the
control system and tune all PID loops and other control systems Task 20. Field Test at NCCC We will install the prototype test unit at the NCCC and conduct testing
throughout a 3 week test campaign (750 hrs) The task also includes the de-commissioning of the unit and its shipment to
the Wabash River IGCC plant for further evaluations
TDA R e s e a r c h
BP3 – Tasks (Cont’d)
56
Task 21. Field Test at Wabash River IGCC Plant TDA will work with CB&I to install the slipstream test unit Test unit will be evaluated in a 2-3 month campaign using synthesis gas
generated from an oxygen-blown gasifier Following shakedown runs, we will perform a series of tests to evaluate
system’s performance at different operating conditions A minimum of 1,440 hours testing is scheduled Task 22. System Analysis Using the most recent reactor design data and feedback from CB&I, we will
update the Aspen-PlusTM process model developed in a previous DOE/NETL project
We will estimate of COE using DOE Guidelines for Carbon Capture and Sequestration (January 2011 dollars)
TDA R e s e a r c h
BP3 – Milestone Log and Decision Points
57
BP ID Task No. Title Description
Planned Completi- on Date
Verification Method
3 3-1 19 Shakedown Testing of Integrated Skid
Complete the Shakedown tests using simulated
gases 12/31/2016 Results update
3 3-2 20 Field Tests at NCCC Complete Field Tests at NCCC 3/31/2017 Site Approved SOP
for the test skid
3 3-3 17 Process Design Complete the full-scale system & process design 9/29/2017 Results update
3 3-4 18 Long-term Durability Target III
Complete up to 30,000 cycles at bench-scale 9/29/2017 Results update
3 3-5 21 Field Tests at Wabash River IGCC
Complete Field Tests at Wabash River IGCC 9/29/2017 Results update
3 3-6 22 System Analysis Complete System and Cost Analysis 9/29/2017 Results update
3 3-7 1 Final Review Meeting Present the BP3 results to DOE/NETL 9/29/2017 Presentation file
Project Completion 9/29/2017
TDA R e s e a r c h
Decision Points – Project Completion
58
Decision Point Date Success Criteria
Project Completion 9/29/2017
Complete 30,000 cycles in the life test with less than 5% degradation per 10,000 cycles in sorbent performance.
Complete a minimum of 2,000 hours of testing with Pilot Scale Unit under coal derived syngas (total including both air blown and oxygen blown gasifier conditions) while achieving 90% carbon capture with 95% CO2 purity under oxygen blown gasification conditions.
Increase in COE is 20% lower than that of the SelexolTM based CO2 capture Systems and Cost of CO2 captured based on June 2011$ basis is less than $40/tonne with 95+% CO2 purity.
TDA R e s e a r c h
Deliverables & Briefings
59
TDA will provide Periodic Quarterly, Topical, and Final reports in accordance with the "Federal Assistance Reporting Checklist“ Test plan for NCCC Field Test Test Plan for Wabash River Field Test Post-Test analysis of NCCC Field Testing Post-Test analysis of Wabash River Field Testing Techno-economic analysis as defined in Attachment 1 to the SOPO
TDA will prepare detailed briefings for presentation to the Project Officer at the Project Officer’s facility located in Pittsburgh, PA or Morgantown, WV Briefings will be arranged with the DOE Project Officer, one at project
kick-off and one at the end of each BP A final project briefing at the close of the project will also be given TDA will present a technical paper(s) at a National conference such as
MEGA Symposium or The National Meeting of the American Chemistry Society each year upon approval of the DOE Technical Monitor
TDA R e s e a r c h
Project Budget
60
TDA R e s e a r c h
Project Team Organization
61
TDA R e s e a r c h
Risk Management
62
Description of Risk Probability Impact Risk Management (Mitigation and Response Strategies)
Technical Risks:
Heat Management not providing the expected performance of 5°C or lower temperature rise in the beds
Low Moderate
TDA will be using CFD models and validate models to develop the heat management concepts and design the advanced reactors.
Advanced reactor designs resulting in high capital costs and complex control schemes
Low High TDA will be looking designs that would have a low impact on the capital costs and
Resource Risks:
Demonstration site availability Low Low
TDA will get both NCCC and Wabash River IGCC plant involved early and get the necessary approvals we will also look for other options for backup
Advanced reactor design fabrication & testing Low Moderate
We will plan ahead and stay ahead of schedule to give us ample time to deal with delays or problems
Management Risks:
Communication & co-ordination Low Low
TDA will have regular meetings and teleconferences to keep the entire team involved and informed on the project progress.
JDA & NDA between partners Low Moderate TDA has prior experience with the partners so we will be able to get the JDA and NDA executed on time